PROCESS FOR FLUORINATED PROPANES AND PENTANES

Abstract: The instant invention relates to producing fluorinated propanes and pentanes. More particularly it relates to producing perhalofluoropropanes and pentanes by reacting dihalodifluoromethanes with polyfluoroethylenes, notably tetrafluoroethylene (TFE) and chlorotrifluoroethylene (CTFE) while in the presence of an aluminum chlorofluoride catalyst.

Description: TITLE PROCESS FOR FLUORINATED PROFANES AND PENTANES FIELD OF THE INVENTION The instant invention relates to producing fluorinated propanes and pentanes. More particularly it relates to producing perhalofluoropropanes and pentanes by reacting dihalodifluoromethanes with polyfluoroethylenes, notably tetrafluoroethylene (TFE) and chlorotrifluoroethylene (CTFE) while in the presence of an aluminum chlorofluoride catalyst. In another aspect, the instant invention relates to preparing novel perbromofluoroalkanes containing three, or five carbon atoms. In still another aspect, the instant invention relates to a process for converting the perhalofluorocarbons to hydrofluorocarbons(HFCs) by reaction with a source of active hydrogen effective to convert one or more carbon- nonfluorohalogen bonds to carbon-hydrogen bonds. Thus, the perhalofluoropropanes and pentanes, products of the inventive process, are potentially useful for manufacturing hydrofluorocarbons which, in turn, in view of their inherently low ozone depletion potentials, are environmentally attractive alternatives for perchlorofluorocarbons (CFC's) in such established uses as refrigerants, expansion agents, aerosol, propellants, fire extinguishing agents, power cycle working fluids, polymerization media, heat transfer media, solvents, carrier fluids, cleaning and drying agents, gaseous dielectrics, among other applications. BACKGROUND OF THE INVENTION Joyce, U. S. Patent No. 2,462,402 (Feb. 22, 1949) discloses a process for the production of highly halogenated fluoroalkanes which comprises contacting TFE with a polyhalogenated alkane,preferably a methane, containing at least one chlorine atom and no more than two fluorine atoms, in the presence of a polyvalent metal halide catalyst, preferably aluminum chloride. U. S. Patent No.2,462,402, to Coffman, et. al., is referenced in the Journal of the American Chemical Society, Vol. 71, pages 979-980 (1949) which discloses that reacting CHC1F2 (chlorodifluoromethane) while in the presence of aluminum chloride with TFE produces CHC12F5 having one less F atom than the sum of fluorine atoms in the reactants. Likewise, CHC1F2 reacting with CTFE yields CHC13F4. Paleta, in a review article "Fluorine Chemistry Reviews", Vol. 8, page 51 (1977) states: The ionic addition reactions of fluoromethanes in the presence of aluminum chloride are limited to the monofluoro derivatives only. When in contact with aluminum chloride, both difluorodichloromethane and difluorochloromethane were found to undergo a rapid disproportionation with the formation of monofluorochloromethanes (along with some further compounds) that are able to add to fluoroethylenes.". The disclosure of each of the previously identified references is hereby incorporated by reference. SUMMARY OF THE INVENTION One aspect of this invention relates to a process for producing valuable perhalopolyfluoropropanes and pentanes from known dihalodifluoromethanes, particularly dichlorodifluoromethane, and polyfluoroethylenes, such as tetrafluoroethylene (hereinafter referred to as "TFE") and chlorotrifluoroethylene (hereinafter referred to as "CTFE"). Another aspect of the invention provides such a process that produces propanes and pentanes wherein the total number of fluorine atoms is equal to the sum of the number of fluorine atoms in the dihalodifluoromethane reactant and the number of fluorine atoms in the polyfluoroethylene reactant. Still another aspect of the invention relates to novel perbromofluoropropanes and pentanes. A still further aspect of the invention relates to a process for obtaining hydropolyfluoropropanes and pentanes having relatively low ozone depletion potentials wherein carbon-nonfluorohalogen bonds, e.g., C-Cl or C-Br bonds, of the perhalofluoropropanes and pentanes are converted to carbon-hydrogen bonds. Notwithstanding conventional beliefs as described in Paleta, the instant invention can react dihalodifluoromethanes, wherein the halo corresponds to non-fluoro halogens, with TFE and/or CTFE to produce perhalofluoropropanes and/or pentanes, wherein the total number of fluorines in said propanes and pentanes is equal to the sum of the fluorines in the methanes and fluoroolefins being reacted. The process of the invention comprises producing perhalofluoropropanes and/or pentanes by: (i) contacting (a) a dihalodifluoromethane, CXYF2, wherein X and Y are independently Cl or Br, with (b) at least one of tetrafluoroethylene and chlorotrifluoroethylene while in the presence of (c) a catalytic amount of an effective aluminum chlorofluoride, at a temperature and pressure effective to result in the formation of (d) at least one of a perhalofluoropropane having 5 to 6 fluorine atoms and 2 to 3 nonfluorohalogen atoms, e.g., bromine and/or chlorine atoms, and a perhalofluoropentane having 8 to 10 fluorine atoms and 2 to 4 nonfluorohalogen atoms, e.g., bromine and/or chlorine atoms; the total number of fluorine atoms in said propane and/or pentane products being the sum of the number of fluorine atoms in the dihalodifluoromethane and the number of fluorine atoms in the TFE and/or CTFE, and; (ii) recovering at least one of said propanes and pentanes. In one aspect of the invention, the dihalodifluoromethane comprises CC12F2 (CFC-12), the fluoroethylene comprises TFE and the aluminum chlorofluoride contains about 3 to about 64% F by weight, normally about 16 to 61 % F by weight. Such aluminum chlorofluorides, which correspond to AlC13-xFx, wherein x is typically about 1.0 to about 2.8, are hereinafter referred to as "modified aluminum chlorides". Modified aluminum chlorides are conveniently prepared by reacting commerically available anhydrous A1C13 with one or more chlorofluorocarbons, hydrochlorofluorocarbons, or hydrofluorocarbons as disclosed in U.S. Patent No. 5,157,171 to Sievert, et. al. at column 4 line 2 through column 5 line 4, the entire disclosure of which is hereby incorporated herein by reference. In one embodiment of the invention, the reaction conditions, e.g., the mole ratios of reactants, their feed rates, and temperature and pressure, are controlled so as to favor a one-to-one reaction of the dihalodifluoromethane with the fluoroolefin, while in the presence of a modified aluminum chloride catalyst, and result in the formation of halofluoropropanes as the predominant products as illustrated by equation (1). (1) CC12F2 + CF2=CF2 -> C3C12F6, e.g., CC12FCF2CF3. In another embodiment, the reaction conditions are adjusted for promoting production of halofluoropentanes as the predominant products via a one- to-two reaction stoichiometry, while in the presence of a modified aluminum chloride catalyst, as illustrated in equation (2). (2) CC12F2 + 2 CF2=CF2 -> C5C12F10, e.g., C2F5CC12C2F5. In still another aspect of the invention, the reaction products, as perhalofluoropropanes and/or as perhalofluoropentanes are treated with one or more reducing means under conditions effective for converting the non-fluorohalide groups of the propanes and pentanes, i.e., the -CXY- groups, wherein X and Y are independently Cl or Br, to -CHX- or -CH2- groups, usually the latter. The reducing means include photochemical reducing means, chemical reducing means, catalytic hydrogenation reducing means, among other suitable means. DETAILED DESCRIPTION In accordance with the present invention one or more perhalofluoropropanes comprising (A) C3XYF6, when produced from TFE, (B) C3C1XYF5, when produced from CTFE, and perhalofluoropentanes having the formula C5XYFiO, when produced from TFE, (C) C5C12XYF8, when derived from a mixture of TFE and CTFE; wherein X and Y stand for Cl or Br as defined above, can be prepared by reacting CXYF2, e.g., CC12F2, with TFE and/or CTFE in the presence of a modified aluminum chloride catalyst. The reactions may be represented by equations (1) and (2) above, illustrated with CC12F2 and TFE as the reactants. The CXYF2 starting materials for the process of this invention can be selected from at least one member selected from the group of CC12F2, CBrClF2, and CBr2F2. The fluoroolefin starting materials for the process of this invention are selected from one or more of CTFE (CC1F=CF2) and TFE (CF2=CF2). The combination of these CXYF2 starting materials with these fluoroolefin starting materials in the presence of a modified aluminum chloride catalyst permits making reaction products selected from one or more of C3C14F4 isomers including CC13CF2CC1F2 and CC13CC1FCF3; C3BrC13F4 isomers including CC12FCF2CBrClF; C3Br4F4 isomers including CBr3CF2CBrF2; C3C13F5 isomers including CC1F2CC12CF3, CC1F2CC1FCC1F2, CC12FCC1FCF3, CC12FCF2CC1F2, and CC13CF2CF3; C3BrC12F5 isomers including CF3CBrClCClF2, CClF2CF2CBrClF, CClF2CClFCBrF2, CBrC12CF2CF3 and CBrF2CF2CC12F; C3Br2ClF5 isomers including CBr2ClCF2CF3; C3Br3F5 isomers including CBr3CF2CF3 and CBrF2CBr2CF3; C3C12F6 isomers, including CC12FCF2CF3 and CC1F2CF2CC1F2; C3BrClF6 isomers, including CBrClFCF2CF3, CBrF2CF2CClF2, and CF3CBrClCF3; C3Br2F6 isomers, including CBr2FCF2CF3, CBrF2CF2CBrF2, and CF3CBr2CF3; C5C14F8 isomers, including CF3CC1FCC12CC1FCF3, CC1F2CC1FCF2CC12CF3, and CC1F2CF2CC12CF2CC1F2; C5BrC13F8 isomers; C5Br2C12F8 isomers; C5C13F9 isomers including CClF2CF2CC12CF2CF3,C5BrC12F9 isomers; C5Br2ClF9 isomers;C5Br3F9 isomers including CBrF2CF2CBr2CF2CF3; C5C12F10 isomers including C2F5CC12C2F5 and CF3CC12CF2CF2CF3; C5BrClF10 isomers including C2F5CBrClC2F5 and CF3CBrClCF2CF2CF3; and C5Br2F10 isomers including C2F5CBr2C2F5 and CF3CBr2CF2CF2CF3. Novel perhalofluoropropanes and pentanes that can be produced by using the inventive process comprise at least one member from the group of CClF2CF2CBrClF, CBrC12CF2CF3 and CBrF2CF2CC12F; CBr3CF2CF3 and CBrF2CBr2CF3; CC1F2CC1FCF2CC12CF3 and CC1-F2CF2CC12CF2CC1F2; C5Br2C12F8 isomers; CC1F2CF2CC12CF2CF3, C5BrC12F9 isomers; C5Br2ClF9 isomers; CBrF2CF2CBr2CF2CF3; C2F5CC12C2F5 and CF3CC12CF2CF2CF3; C2F5CBrClC2F5 and CF3CBrClCF2CF2CF3;C2F5CBr2C2F5 and CF3CBr2CF2CF2CF3. Such novel perhalofluoroalkanes can be used for making useful hydrofluorocarbons (HFCs) such as hydrofluoropropanes and hydrofluoropentanes. Such HFCs can be used as refrigerants, blowing agents, cleaning compositions, among other applications. The process of equation (1) indicates a stoichiometry of one mole of CXYF2 per mole of TFE (or CTFE); however, an excess of either reactant may be used as desired with excess of the fluoroolefin promoting formation of the C5 product. Even at mole ratios of about 1:1 however, significant quantities of C5- product can be produced (equation (2)) along with C3-product (equation (1)). The relative proportions of the two reactants can be varied widely for producing a desired product or product mixture of products. Generally, the mole ratio may vary from about 3 to 1 moles of CXYF2 component per mole of the fluoroolefin, to promote C3 production and from about 3 to 1.5 moles of the fluoroolefin per mole of the CXYF2 to promote C5 production. In some cases, CC12F2 may also be employed in the formation of modified aluminum chloride, as defined above, use of sufficient excess enables the production of modified aluminum chloride in situ from anhydrous aluminum chloride so that the catalyst modification reaction need not be carried out as a separate step. The ability to form the modified catalyst in situ constitutes an improvement over the art because the process can be practice by using A1C13 thereby obviating a modified catalyst formation step. It is, however, important that the excess quantity, for example, of CC12F2, avoids converting the AlClx-3Fx to A1F3 which in turn can adversely effect the inventive process. In some cases, the CC12F2 and TFE and/or CTFE can be simultaneously contacted with the A1C13. The process can be conducted batchwise or in a continuous manner. In the continuous mode, a mixture of dihalodifluoromethane and fluoroolefin is passed through or over a bed or body of modified aluminum chloride which may be under agitation at suitable temperature and pressure to form a product stream, and the desired products are recovered from the stream by conventional methods such as fractional distillation. In some cases, the reactants can be added individually or simulataneously. In the batch process, the reactants and catalyst may be combined in a suitable commercially available reactor to form a reaction mixture and the mixture held at a suitable temperature and pressure, normally under agitation, until a desired degree of conversion to the desired propanes and/or pentanes is attained. In one embodiment, the reactor is initially charged with the catalyst, and optionally with a diluent, then the dihalodifluoromethane and the fluoroolefin, as separate streams or as a combined stream, in a desired mole ratio, are fed into the reactor at a controlled rate and maintained therein until the reaction is substantially complete. If the reactor is fed with dihalodifluoromethane and catalyst in the substantial absence of fluoroolefin, then the system (reactor and ingredients) should be kept relatively cold, e.g., between about -78C and IOC, to minimize disproportionation of the dihalodifluoromethane to higher and lower fluorine content methanes. The process may be practiced with or without a solvent or reaction diluent. Such material, if used, must be substantially inert to the reactants and catalyst, and also should boil at a temperature enabling separation from the propane and pentane reaction products. Representative of such solvents comprise at least one member from the group of CC14, CF3CHC12, CC13CF3, propane and pentane products of the present invention process, e.g., CF3CF2CC12F, CC1F2CF2CC1F2, CF3CF2CC12CF2CF3, CF3CC12CF2CF2CF3, and isomers, among others. The reaction temperature may be varied, and normally is in the range of from about OC to about 150C, usually in the range of from about 20C to about HOC. The reaction pressure likewise may vary widely from subatmospheric to superatmospheric; but normally the reaction is carried out at elevated pressures, particularly at pressures generated autogenously in conformity with the reaction temperature employed. The pressure may be controlled by adjusting the amount of unreacted dihalodifluoromethane and fluoroolefin. The reaction time, or time necessary for sufficient substantially complete reaction, can vary with the temperature chosen for the reaction. In general the higher the temperature the shorter the reaction time. The degree of reaction, however, is easily determined by the change in the autogenous pressure in the reaction vessel, because the pressure drops as the reaction proceeds, so that the time at which the pressure stops decreasing can be taken as the end of the reaction period. The reaction time can also vary with the quantity or volume of reactants in the reactor. Generally, the reaction time, is in the range of from about 0.25 h to about 8.0 hours are normally employed temperature ranges. The amount of modified aluminum chloride generally employed is in the range of from about 1 to 20 percent based on the weight of the dihalodifluoromethane reactant. The reaction products may be recovered from the reactor by using any suitable conventional means such as by filtration or distillation. It is usually convenient to decompose the catalyst by treatment with water and then recover the product by distillation. If desired, the perhaloproducts of the invention process may be hydrodehalogenated to hydro-derivatives comprising at least one hydrogen substituent and correspondingly one less nonfluorohalogen substitutent than present in the starting perhalofluorocarbon by being treated with one or more reducing means. Examples of suitable reducing means comprise at least one of photochemical, chemical, and normally catalytic hydrogenation means. Catalytic hydrogenation may generally be effected with molecular hydrogen over a suitable catalyst, typically a Group VHI metal, as disclosed, for example, in Smith, U. S. Patent No. 2,942,036 and Rao, U. S. Patent No. 5,136,113; the entire disclosures of which are incorporated herein by reference. Catalytic hydrogenation can be practiced in the liquid or vapor phase. Normally, the vapor phase is employed with a catalytic metal such as palladium that can be supported on carbon or alumina; usually the latter. Catalytic hydrogenation may generally be effected with molecular hydrogen over a suitable catalyst, typically a Group Vm metal, as disclosed, for example, in Smith, U. S. Patent 2,942,036 and Rao, U. S. Patent 5,136,113 which disclosures are incorporated herein by reference. Hydrogenation can also be conducted in the vapor phase with a catalytic metal such as nickel, palladium, platinum, rhodium, iridium, among others. The catalytic metal is normally supported on a suitable carrier such as carbon or alumina. The use of alumina as a support for palladium is particularly desirable for hydrodechlorination and hydrodebromination as illustrated in Example 22 for the conversion of CF3CF2CC12CF2CF3 to CF3CF2CH2CF2CF3. The use of carbon as _ a support for palladium is effective for hydrogenating, when a combination of hydrodehalogenation, dehydrofluorination, and hydrogen addition is desired as illustrated in Examples 20 and 21 for the conversion of CF3CF2CC12CF2CF3 to CF3CHFCH2CF2CF3. The hydrodehalogenation reactions of the present invention may be conducted at temperatures between about 25C and 250C, normally between about 50C and 200C, and typically between about 100C and 200C. The choice of optimum hydrodehalogenation temperature will be dictated by whether the halogen being removed or replaced is chlorine or bromine, the desired degree of conversion of the perhalofluoroalkane starting material, the percent loading of the active metal upon the support, among other factors. Perbromofluoroalkanes are more readily hydrodehalogenated than are perchlorofluoroalkanes. The hydrodehalogenation reactions may be operated at pressures between atmospheric and 100 psig or higher. The choice of pressure may be dictated by the vapor pressure of the reactants, intermediates, and products. The ratio of hydrogen to perhalofluoroalkane employed in the dehydrohalogenation reaction may vary from about 0.5 to about 10 on a molar basis, and usually should be from about 1 to 4. Relatively large excesses of hydrogen can be employed. A deficiency of hydrogen may be used to control the conversion rate of the perhalofluoroalkane if desired. The products of the hydrodehalogenation reaction may be separated from excess hydrogen, if any, and HF, HC1, and/or HBr by-products by normal distillation or neutralization techniques. The products of the hydrodehalogenation comprise at least one member from the group of hydrofluoroalkanes, hydrofluoroalkenes, hydrohalofluoroalkanes, and hydrohalofluoroalkenes. Examples of hydrodehalogenation products from the hydrodechlorination of CF3CF2CC12CF2CF3 (see Examples 20, 21, and 22) comprise at least one of CF3CF2CH2CF2CF3, CF3CHFCH2CF2CF3, CF3CF=CHCF2CF3, CF3CF2CHC1CF2CF3, CF3CF=CC1CF2CF3, among others. The hydrohalofluoroalkanes, hydrofluoroalkenes, and hydrohalofluoroalkenes are intermediates in the formation of the hydrofluoroalkanes and may be separated from the hydrofluoroalkanes for conversion to the saturated products. Hydrofluoropropanes and hydrofluoropentanes produced by hydrodehalogenation of the perhalofluoroalkanes comprise at least one of C3H4F4 isomers including CH3CF2CHF2, CH3CHFCF3, and CH2FCF2CH2F; C3H3F5 _ _ isomers including CHF2CH2CF3, CHF2CHFCHF2, CH2FCHFCF3, CH2FCF2CHF2, and CH3CF2CF3; C3H2F6 isomers including CH2FCF2CF3, CHF2CF2CHF2, and CF3CH2CF3; C5H8F4 isomers including CHF2CH2CH2CH2CHF2; C5H7F5 isomers including CHF2CH2CH2CH2CF3, and CHF2CHFCH2CH2CHF2; C5H6F6 isomers including CF3CH2CH2CH2CF3, CHF2CH2CHFCH2CF3, CHF2CHFCH2CH2CF3, and C-HF2CF2CH2CH2CHF2; C5H5F7 isomers including CF3CH2CH2CΗFCF3, CHF2CHFCHFCH2CF3, CHF2CF2CH2CHFCHF2, CHF2CF2CH2CH2CF3, and CHF2CH2CH2CF2CF3; C5H4F8 isomers including CF3CHFCH2CHFCF3, CHF2CHFCF2CH2CF3, CHF2CF2CH2CF2CHF2, CHF2CF2CH2CHFCF3, CF3CH2CH2CF2CF3, and CHF2CHFCH2CF2CF3; C5H3F9 isomers including CF3CHFCH2CF2CF3, CF3CH2CHFCF2CF3, and CΗF2CF2CH2CF2CF3, C5H2F10 isomers including C2F5CH2C2F5 and CF3CH2CF2CF2CF3. Novel hydrofluoroalkanes comprise at least one member from the group consisting of CHF2CH2CH2CH2CHF2; CHF2CH2CH2CH2CF3 and CHF2CHFCH2CH2CHF2; CHF2CH2CHFCH2CF3, CHF2CHFCH2CH2CF3, and CHF2CF2CH2CH2CHF2; CF3CH2CH2CHFCF3, CHF2CHFCHFCH2CF3, CHF2CF2CH2CHFCHF2, CHF2CF2CH2CH2CF3, and CHF2CH2CH2CF2CF3; CF3CHFCH2CHFCF3, CHF2CHFCF2CH2CF3, CHF2CF2CH2CF2CHF2, CHF2CF2CH2CHFCF3, and CHF2CHFCH2CF2CF3; CHF2CF2CH2CF2CF3. All of the above hydrofluoroalkanes can be used in the manner described above in connection with HFCs such as refrigerants, blowing and cleaning agents, among other applications. In addition to hydrogenation, suitable chemical reducing means that may be used include reducting with zinc in the presence of an alcohol as disclosed, for example, by Morikawa, et. al., in International Patent AppUcation 90/08753, and by Krespan in U. S. Patent No.4,935,558; reduction with a complex metal hydrides as disclosed by Clayton in European Patent Application Publication No. 0508,631; reduction with hydrogen iodide or with H2 in the presence of iodine or hydrogen iodide as disclosed by Anton in U. S. Patent No. 5,208,396; the entire disclosure of which are hereby incorporated herein by reference. Suitable photochemical reducing means include reaction of the perhalocompound with alcohols in the presence of ultraviolet light as disclosed by Posta, et. al., in Czechoslovak Patent No. 136,735. The various aspects of this invention may are more readily understood by reviewing the following examples that are provided to illustrate not limit the scope of the appended claims. Examples 1 to 7 illustrate reacting CC12F2 (CFC-12) with CF2=CF2 (TFE) catalyzed by separately prepared modified aluminum chloride catalyst while Example 8 utilizes initially unmodified A1C13 as the catalyst. Examples 8 to 16 utilize CBrClF2 and CBr2F2 as the dihalodifluoromethane reactant, with Example 16 showing the effect of using initially unmodified A1C13 as the catalyst. Examples 17 to 19 illustrate the use of CC1F=CF2 (CTFE) in place of TFE. Examples 20-22 illustrate preparing hydrofluorocarbons from perhalofluoropropanes and pentanes utilizing catalytic hydrogenation. Analyses of reaction products, generally mixtures, were carried out using standard GC/GC-MS and 19F NMR methods, the abbreviations GC, GC-MS, and NMR standing for gas chromatography, gas chromatography-mass spectrometry, and nuclear magnetic resonance spectroscopy. Results are presented in GC area percents unless otherwise indicated with amounts less than about 1% generally omitted. EXAMPLE 1 Reaction of CFC-12 with Tetrafluoroethylene A 400 mL "Hastelloy" C shaker tube was charged with CC13F- modified aluminum chloride (3.0 g). The tube was sealed, cooled to -78C, evacuated, and purged with nitrogen three times. The reactor was then charged with CC12F2 (50 g, 0.41 mole). The cold reactor was placed in the barricaded enclosure, and charged with 25 g (0.25 mole) of TFE. The reactor was warmed to 60C over the course of 0.25 h; during this time the pressure rose to 80 psig. The temperature was held at 60C for 1.3 h (pressure = 80-85 psig) and then raised to 80C and held for 1 h (pressure = 112-116 psig). The following day the reactor was discharged to afford 54.7 g of a clear supernatant over a brown solid. Analysis of the product by GC/GC-MS and 19F NMR indicated the following composition: Component GC Area % Mole % CC12F2 1.3 - CC12FCF2CF3 68.5 53.5 CC1F2CF2CC1F2 * 13.9 CCBF 0.1 - C2F5CC12C2F5 26.5 29.8 CCBCF2CF3 2.1 2.8 CC12FCF2CC1F2 0.2 - CC14 0.8 _ *C3C12F6 isomers were not separated by GC. Noteworthy are the substantial yields of the hexafluorides, CC12FCF2CF3 and CC1F2CF2CC1F2, and the decafluoride, CF3CF2CC12CF2CF3. Also, the appearance of CCBF and CC14 along with the pentafluorides, CCBCF2CF3 and CC12FCF2CC1F2, probably derived therefrom, indicates some disproportionation of the starting CFC-12 reactant had occurred. The modified aluminum chloride catalyst of Example 1 was prepared as foUows: A 500 mL three neck round bottom flask containg a PTFE-coated stirring bar was charged with 50 g of aluminum chloride (A1CB) in a dry box. The flask was passed out of the dry box and fitted with an addition funnel and a dry ice condenser connected to a nitrogen bubbler. The addition funnel was charged with 175 mL of CCBF and the condenser was fiUed with a methanol/dry ice mixture. The CCBF was gradually added to the flask and the mixture began to reflux vigorously. The reaction continued to reflux for a hour after all of the CCBF had been added. The reaction was not heated. GC analysis of the supernatant Uquid indicated it was essentially pure CC14. The mixture was stirred overnight at ambient temperature and then volatiles were removed in vacuum. The resulting solid was dried under dynamic vacuum to afford 22 g of off-white powder. Analysis: weight % F = 57.8; this corresponds to a composition that is approximately A1C10.3F2.7. EXAMPLE 2 Reaction of CFC-12 with Tetrafluoroethylene A 400 mL "Hastelloy" C shaker tube was charged with CCBF- modified aluminum chloride (1.5 g). The reactor was sealed, cooled to -78C, evacuated, and purged with nitrogen three times. The reactor was then charged with CC12F2 (40 g, 0.33 mole). The cold reactor was placed in the barricade and charged with 15 g (0.15 mole) of TFE. The reactor was warmed to 30C over the course of 0.5 h and the pressure rose to 40 psig. TFE was then added to the reactor in 5 g increments at at temperature of 31-32C until a total of 50 g (0.50 mole) had been added; the pressure gradually rose to 114 psig. The reactor was then held at a temperature 31-2C for 3 h; the final pressure was 59 psig. The following day the reactor was discharged to afford 54.7 g of a clear supernatant over a brown soUd. Analysis of the product by GC/GC-MS and 19F NMR indicated the following composition: Component GC Area % CC1F2CF2C1F2/CC12FCF2CF3 12.6 CF3CC12CF2CF2CF3 .0 CF3CF2CC12CF2CF3 83.7 C3CBF5 isomers 1.0 C5CBF9 isomers 0.9 The modified aluminum chloride catalyst of Example 2 was prepared following a procedure similar to that described in Example 1 except that the reaction volatiles were removed promptly after the reaction ceased to reflux. Analysis: weight % F = 47.7; weight % Al = 26.6; this corresponds to a composition that is approximately A1C1F2. EXAMPLE 3 Reaction of CFC-12 with Tetrafluoroethylene A 400 mL "HasteUoy" C shaker tube was charged with CCBF- modified aluminum chloride (4 g) and 128 g of CC13CF3 as a diluent. The reactor was sealed, cooled to -78C, evacuated, purged with nitrogen three times, and charged with CC12F2 (50 g, 0.41 mole). The cold reactor was placed in the barricade and charged with 20 g (0.20 mole) of TFE. The reactor was warmed to 30C over the course of 0.25 h and the pressure rose to 45 psig. TFE was then added to the reactor in 5 g increments at a temperature of 29-30C over the next 1.5 h until a total of 50 g (0.50 mole) had been added; the pressure gradually rose to 42 psig. The reactor was then held at a temperature 30C for 3 h; the final pressure was 20 psig. The foUowing day the reactor was discharged to afford 228.1 g of a clear _ _ supernatant over a dark solid. Analysis of the product by GC indicated the following composition: Component GC Area % CC1F2CF2CC1F2/CC12FCF2CF3 18.3 CCBCF3 55.1 CF3CC12CF2CF2CF3 0.3 CF3CF2CC12CF2CF3 21.2 C3CBF5 isomers 2.1 CC14 0.7 C5CBF9 isomers 0.8 The modified aluminum chloride catalyst of Example 3 was prepared as follows: A I L four neck round bottom flask was charged with 150 g of aluminum chloride (AICB) in a dry box. The flask was passed out of the dry box and fitted with an addition funnel, a mechanical stirrer, a thermocouple, and a dry ice condenser connected to a nitrogen bubbler. The addition funnel was charged with 410 g of CCBF and the condenser was fiUed with a methanol/dry ice mixture. The CCBF was added to the flask over the course of about 1 h. After the addition was complete, the mixture was stirred for 1 h and then volatiles were removed in vacuum. The resulting solid was dried under dynamic vacuum with gentle warming (70C water bath) to afford 120.6 g of pale yeUow powder. Analysis: weight % Al = 25.5; this corresponds to a composition that is approximately A1C11.3F1.7. EXAMPLE 4 Reaction of CFC-12 with Tetrafluoroethylene Example 3 was repeated with the exception that CHC12CF3 was used as the diluent (120 g). After charging with CC12F2, the cold reactor was placed in the barricade and charged with 15 g (0.15 mole) of TFE. The reactor was warmed to 29C over the course of 0.25 h and the pressure rose to 65 psig. TFE was then added to the reactor in 5 g increments at at temperature of 27-33C over the next 1.3 h until a total of 50 g (0.50 mole) had been added; the pressure gradually rose to 105 psig. The reactor was then held at a temperature 30-38C for 3 h; the final pressure was 58 psig. The following day the reactor was discharged to afford 205.4 g of a clear supernatant over a dark solid. Analysis of the product by GC indicated the following composition: Component GC Area % CC1F2CF2C1F2/CC12FCF2CF3 20.6 CHC12CF3 59.3 CF3CC12CF2CF2CF3 0.2 CF3CF2CC12CF2CF3 16.8 C3CBF5 isomers 1.8 C5CBF9 isomers 0.7 EXAMPLE 5 Reaction of CFC-12 with Tetrafluoroethylene A 400 mL "HasteUoy" C shaker tube was charged with aluminum chloride (2 g, 0.015 mole). The reactor was sealed, cooled to -78C, evacuated, purged with nitrogen three times, and charged with CC12F2 (50 g, 0.41 mole). The cold reactor was placed in the barricade and charged with 25 g (0.25 mole) of TFE. The reactor was warmed to 59C over the course of 0.3 h and the pressure rose to about 230 psig. The reactor was held at a temperature 52-60C for 3 h; the final pressure was 134 psig. The reactor was discharged to afford 41.1 g of a clear supernatant over a brown soUd. Analysis of the product by GC/GC-MS indicated the foUowing composition: Component GC Area % CC1F2CF2C1F2/CC12FCF2CF3 51.5 CF3C12CF2CF2CF3 0.5 CF3CF2C12CF2CF3 14.8 CCBC2F5 22.0 CC12FCF2CC1F2 5.4 CC1F2CF2CC12C2F5 3.1 CC12=CC12 0.8 The formation of CCBC2F5 in such a substantial amount in the presence of initially unmodified AICB, the .amount being significantly greater than that produced in the presence of initially modified aluminum chloride catalyst (Examples 1-4), indicates disproportionation of CC12F2 had occurred to CCBF (among other products) followed by addition of CCBF to TFE. Further, it can be seen, in general, in comparison with the results of Examples 1-4, that the yields of the desired C3C12F6 and C5C12F10 products are lower than those obtained starting with an initially modified catalyst. The not insignificant yields of C3C12F6 and C5C12F10 products in Example 5 are beUeved the result of employing CC12F2 in excess over the stoichiometric quantity. EXAMPLE 6 Reaction of CC12F2 with TFE - Continuous Process A I L stainless steel, stirred autoclave was charged with 10 g of AlCB-xFx modified -aluminum chloride. The autoclave was sealed and evacuated and 100 g of CCBCF3 were drawn into the autoclave under vacuum. At a temperature of 13C and a pressure of 4 inches of vacuum, 20 g of TFE were fed to the autoclave. At an initial temperature and pressure of 10.9C and 32.3 psig, TFE and CC12F2 were then co-fed to the reactor at rates of 50 g/h and 37.5 g/h, respectively as the reactor temperature was brought to 30-3 IC. Gas feeds was continued until the pressure reached 150 psig (31C); 2.98 moles of TFE had been fed and 2.00 moles of CC12F2 had been fed. After stirring for 3.5 h, the reaction was shut down and 502 g of product were discharged. GC analysis of the product indicated the foUowing major products: Component GC Area % CC1F2CF2CC1F2/CC12FCF2CF3 22.6 CF3CC12C2F5 1.8 CC13CF3 15.5 CF3CC12CF2CF2CF3 0.5 CF3CF2CC12CF2CF3 52.0 CCBC2F5 1.9 CC1F2CF2CC12F 0.1 CC14 2.4 C5CBF9 isomers 1.3 The modified aluminum chloride catalyst used in this Example was prepared following a procedure similar to that described in Example 3. Analysis: weight % Al = 26.8; this corresponds to a composition that is approximately A1C11F2. EXAMPLE 7 Reaction of CC12F2 with TFE - Continuous Process A I L stainless steel, stirred autoclave was charged with 10 g of A1C13- xFx. The autoclave was sealed and evacuated and 100 g of CCBCF3 were drawn into the autoclave under vacuum. At a temperature of 16C and a pressure of 2 inch of vacuum, TFE and CC12F2 were co-fed to the autoclave at rates of 80 g/h and 97 g/h, respectively as the reactor temperature was brought to 31-34C. Gas feeds were continued until the pressure reached 149 psig (31C); 3.29 moles of TFE had been fed and 3.90 moles of CC12F2 had been fed. After stirring for 2 h, the reaction was shut down and 551 g of product were discharged. GC analysis of the product indicated the foUowing major products: Components GC Area % CClF2CF2CαF2/CC12FCF2CF3 30.2 CF3CC12C2F5 0.3 CC13CF3 14.0 CF3CC12CF2CF2CF3 0.6 CF3CF2CC12CF2CF3 41.5 CCBC2F5 7.7 CC1F2CF2CC12F 0.8 CC14 0.7 C5CBF9 isomers 2.9 The modified aluminum chloride catalyst used in this Example was prepared following a procedure similar to that described in Example 3. Analysis: weight % Al = 27.1; this corresponds to a composition that is approximately A1C11F2. EXAMPLE 8 Reaction of CBrClF2 with Tetrafluoroethylene A 400 mL "HasteUoy" C shaker tube was charged with CCBF- modified aluminum chloride (6.7 g). The tube was sealed, cooled to -78C, evacuated, and purged with nitrogen three times. The reactor was then charged with CBrClF2 (89.8 g, 0.54 mole). The cold reactor was placed in the barricade and charged with 42 g (0.42 mole) of TFE. The reactor was warmed to 40C over the course of 1 h during this period the pressure rose to 37 psig. The temperature was held at 40C for 1 h (pressure = 38 psig) .and then raised to 80C and held for 2 h; during this time the pressure increased from 82 psig to 100 psig. The reaction was shut down at this point. The following day the reactor was discharged to afford 123.9 g of a orange supernatant over a dark soUd. Analysis of the product by GC/GC-MS and 19F NMR indicated the following composition: Component < jC Area % Mole % CC12F2 0.7 0.8 CBrClF2 2.9 3.2 CBrClFCF2CF3 54.0 39.9 CBrF2CF2CClF2 * 19.1 CCBCF2CF3 0.4 0.3 C5BrClF10 0.4 C2F5CBrClCF2CF3 27.2 24.8 C5Br2ClF9 (2) 0.8 CBr2ClCF2CF3 9.6 11.9 C3BrC12F5 1.6 _ *C3BrC12F6 isomers not separated by GC. The modified aluminum chloride catalyst used in this Example was prepared following a procedure similar to that described in Example 1. EXAMPLE 9 Reaction of CBrClF2 with Tetrafluoroethylene The procedure of Example 8 was repeated using 38 g of TFE (0.38 mole), 30 g of CBrClF2 (0.18 mole), and 3 g of CCBF-modified aluminum chloride (see Example 1). The TFE was added portionwise at a maximum temperature of 36C (maximum pressure = 100 psig). The reaction was held at 36-39C for 1 h and then heated to 79-81C and held at that temperature for 2 h (final pressure = 118 psig). The crude product weighed 58.3 g. Analysis of the product by GC and GC- MS indicated the following composition: Component • GC Area % CBrF2CF2CClF2 14.7 C5BrClF10 1.7 _ _ C2F5CBrClC2F5 75.3 C2F5CBr2C2F5 0.1 C3Br2ClF5 1.3 C5BrC12F9 0.1 C5Br2ClF9 (3) 0.9 EXAMPLES 10. 11. and 12 Reaction of CBr2F2 with TFE using a CCBF-modified aluminum chloride catalyst A 400 mL "HasteUoy" C shaker tube was charged with CCBF- modified aluminum chloride (4 g) and CBr2F2 (63 g, 0.30 mole). The tube was sealed, cooled to -78C, evacuated, and purged with nitrogen three times. The cold reactor was placed in the barricade and charged with 30 g (0.30 mole) of TFE. The reactor was warmed to 100C over the course of 1 h during this period the pressure rose to 50 psig. The temperature was held at 99-101C for 4 h (max. pressure = 60 psig) and then heating and agitation were stopped. The following day the reactor was discharged to afford 91.6 g of a clear supernatant over a dark soUd. The reaction between CBr2F2 and TFE was repeated following the procedure above at at temperature of 60C (EXAMPLE 11) and at a temperature of 30C (EXAMPLE 12). The GC analyses of these runs are compared in the table below. Reaction Products, GC Area % Component Ex. 10 Ex. 11 Ex. 12 CBrF2CF2CBrF2 14.0 13.7 13.7 CBr2FCF2CF3 19.5 3.2 29.3 CBrC12CF2CF3 0.2 0.2 0.3 CF3CBr2CF2CF2CF3 6.2 8.5 0.8 C2F5CBr2C2F5 34.4 57.4 39.7 CBrF2CBr2CF3 19.0 6.3 2.2 CBr3C2F5 0.4 0.06 8.0 C5Br3F9 1.2 1.2 2.1 The modified aluminum chloride catalyst used in Examples 10 and 11 were prepared following a procedure similar to that described in Example 1. Analysis: weight % Al = 27.7; this corresponds to a composition that is approximately A1C10.8F2.2. The modified aluminum chloride catalyst used in Example 12 was the same as that described in Example 1. EXAMPLES 13 and 14 Reaction of CBr2F2 with TFE using a CCBF-modified Aluminum Chloride Catalyst A 400 mL "Hastelloy" C shaker tube was charged with CCBF- modified aluminum chloride (see Example 1; 1 g) and CBr2F2 (42 g, 0.20 mole). The reactor was sealed, cooled to -78C, evacuated, and purged with nitrogen three times. The cold reactor was placed in the barricade, agitation was begun, and 10 g (0.10 mole) of TFE were added. The reactor was warmed to 0C over the course of 19 minutes; during this time the pressure decreased from 37 psig at -27C to 22 psig at 0C. An additional 17 g of TFE was added in five portions over the course of 1.2 h during which time the pressure rose to 61 psig. An additional 6 g of TFE were added bring the total pressure to 92 psig (total of 0.33 mole TFE added) and the reactor held at 30C for 13 h (final pressure = 98 psig). Discharge of the reactor afforded 61.1 g of a yellow supernatant over a brown solid. The reaction of CBr2F2 with TFE was repeated (EXAMPLE 14) using 105 g (0.50 mole) of CBr2F2 and 40 g (0.40 mole) of TFE in the presence of 2 g of CCBF-modified aluminum chloride (see Example 1) at 30C. The results of these two experiments are given in Table below. Product E ►istributii on for Reaction of TFE with 12B2 Ex. 13 Ex. 14 Component GC Area % Mole % GC Area % Mole % CBrF3 0.08 - 0.5 1.2 CBr2F2 0.8 - 0.9 1.3 CBrF2CF2CBrF2 12.8* 20.3 46.8* 24.0 CBr2FCF2CF3 1.5 - * 31.5 CF3CBr2CF3 * 1.7 * 1.1 CF3CBr2CF2C2F5 2.3 1.7 0.7 - C2F5CBr2C2F5 72.6 69.2 29.0 23.3 CBrF2CBr2CF3 2.0 1.9 2.8 3.1 CBr3C2F5 2.4 2.8 14.3 14.6 C2F5CBr2CF2CBrF2 2.2 2.1 1.9 - CBrF2CF2CBr3 - - 0.2 - *GC trace did not separate C3Br2F6 isomers accurately. EXAMPLE 15 Reaction of CBr2F2 with TFE A I L stainless steel, stirred autoclave was charged with 10 g of CCBF-modified aluminum chloride. The autoclave was sealed and evacuated and 500 g (2.38 moles) of chiUed CBr2F2 were drawn into the autoclave under vacuum. TFE was fed to the autoclave at a rate of 2.2 g/min at an initial temperature and pressure of 23C and 1 psig, respectively; the temperature was brought to about 30C. TFE feed was continued until the pressure reached 151 psig (29C). At this point the feed rate was decreased to 1.1 g/min. TFE was fed intermittently to the reactor keeping the pressure at a maximum value of 150 psig. The reaction was shut down after 4.76 moles of TFE had been fed to the reactor. Discharge of the reactor afforded 868 g of product. GC analysis of the product indicated the foUowing major products: Component GC Area % C5BrF9 isomers 0.9 CBrF2CF2CBrF2 13.5 CBr2FC2F5 6.3 CBrC12C2F5 0.8 CF3CBr2CF2C2F5 4.2 CF3CF2CBr2CF2CF3 63.1 C3Br2ClF5 isomer 1.4 CBrF2CF2CBr2F 1.4 CBr3C2F5 3.0 C5Br3F9 isomers 2.1 The modified aluminum chloride catalyst used in this Example was prepared foUowing a procedure similar to that described in Example 3. Analysis: weight % Al = 23.6; this corresponds to a composition that is approximately A1C12F!. EXAMPLE 16 Reaction of CBr2F2 with TFE using AICB Catalyst A 400 mL "Hastelloy" C shaker tube was charged with AICB (99.99%, 2 g, 0.015 mole) and sealed. The tube was cooled to -78C, evacuated, and purged with nitrogen three times. The cold reactor was then charged with CBr2F2 (63 g, 0.30 mole) and placed in the barricade. The reactor was agitated and then charged with 10 g (0.10 mole) of TFE. The reactor was warmed to 31C over the course of 40 minutes as the pressure rose to 94 psig. An additional 20 g of TFE were added in three portions over the next 1.5 h. The temperature was held at 27-32C; the pressure was held at about 100 psig for most of this period, but rose to 162 psig as the last few grams of TFE were added. The reactor was held at about 30C for an additional 6 h as the pressure dropped to 60 psig. The following day, the reactor was discharged to afford 74.2 g of a clear supernatant over a brown soUd. Analysis of the product by GC and GC-MS indicated the foUowing composition: Component GC Area % Mole % CBrClF2 6.4 16.3 CBrF2CF2CClF2 54.8 15.7 CBrClFC2F5 * 41.5 CF3CBrClCF3 * 1.4 CCBCF2CF3 1.7 1.6 CC12FCF2CC1F2 0.4 - C5BrClF10 0.4 - C2F5CBrClC2F5 17.8 13.8 CBrC12C2F5 11.4 8.3 CBrF2CF2CC12F - 1.3 C2F5CBr2C2F5 0.07 - CBr2ClC2F5 3.2 _ *C3BrClF6 isomers not well separated on the GC column employed. EXAMPLE 17 Reaction of CFC-12 with CTFE A 400 mL "Hastelloy" C shaker tube was charged with 2 g of CCBF- modified aluminum chloride. The reactor was sealed, cooled in dry ice, evacuated and purged with nitrogen three times. The reactor was re-evacuated and charged with CFC-12 (50 g, 0.41 mole) and CTFE (35 g, 0.30 mole). The reactor was warmed to 30C and held at 30-39C for 8 h (max pressure, 160 psig at 38C; final pressure, 130 psig at 35C). The product (10.3 g) consisted of a small amount of yellow supernatant over a brown soUd. Analysis of the product by GC, GC-MS, and 19F NMR indicated the following composition. Component GC Area % Mole % cyclo-cis-l,2-C4C12F6 23.1 21.1 cyclo-trans-l,2-C4C12F6 34.2 28.7 CC1F2CC1FCC1F2 1.1 4.0 CC12FCC1FCF3 14.4 15.3 CC1F2CF2CC12F 7.4 11.0 CCBC2F5 * 0.4 CC1F2CC12CF3 * 1.5 C5C14F8 (3 isomers) 18.0 CF3CC1FCC12CC1FCF3 (2 diastereomers) 4.5 CC1F2CC1FCF2CC12CF3 7.8 CC1F2CF2CC12CF2CC1F2 4.2 CCBCF2CC1F2 0.4 0.6 CCBCC1FCF3 0.6 0.7 The modified aluminum chloride catalyst used in this Example was prepared following a procedure siπ-dlar to that described in Example 1. Analysis: weight % Al = 26.6; this corresponds to a composition that is approximately A1C11F2. EXAMPLE 18 Reaction of CBrClF2 with CTFE A 400 mL "HasteUoy" C shaker tube as charged with CCBF-modified aluminum chloride (6.7 g). The reactor was cooled to -78C, evacuated, and purged three times with nitrogen. CBrClF2 (41 g, 0.25 mole) and CTFE (23 g, 0.20 mole) were sequentially condensed into the reactor. The cold reactor was placed in the barricade and agitation was begun. The reactor was heated to 40C and held for 3 h (50 psig) and then heated to 80C and held for 6 h. During the latter stage of the reaction the pressure increased form 80 to 90 psig. The product was discharged to give 55 g of a red-brown supernatant over a Ught-colored soUd. Analysis of the product by GC, GC-MS, and 19F NMR indicated the composition Usted below. Component GC Area % Mole % CF3CBrClCClF2 34.8 48.5 CClF2CF2CBrClF 15.0 23.3 CClF2CClFCBrF2 * 10.4 CC12FCF2CBrClF 13.1 17.7 CBrCUF2 3.3 - CBrF2CClF2 0.7 - CBr2F2 0.3 - C3C12F4 3.9 - CBrF2CBrClF 0.5 - C5CBF7 (4) 3.8 - C4BrC14F7 0.3 - C3BrC12F3 (2) 1.1 - The modified aluminum chloride catalyst of Example 18 was prepared as foUows: A 2 L four neck creased round bottom flask was fitted with an addition funnel, a mechanical stirrer, a thermocouple, and a glycol/water-cooled condenser connected to a nitrogen bubbler. The flask was charged with 200 g of aluminum chloride (AICB). CCBF (700 mL) was added to the flask over the course of about 1 h; during this time the temperature rose to about 67C and gradually dropped to about 50C. After the addition was complete, the mixture was stirred for 1 h. The supernatant was poured off and remaining volatUes were removed under vacuum with gentle warming (70C water bath) to afford 131 g of pale yeUow powder. Analysis: weight % Al = 29.5; this corresponds to a composition that is approximately A1C10.5F2.5. EXAMPLE 19 Reaction of CBr2F2 with CTFE A 400 mL "Hastelloy" C shaker tube was charged with CCBF- modified aluminum chloride (see Example 1; 3 g) and CBr2F2 (54 g, 0.26 mole). The tube was sealed, cooled to -78C, evacuated, purged with nitrogen three times, and then charged with 29 g (0.25 mole) of CTFE. The cold reactor was placed in the barricade and warmed to 30C with agitation; the pressure rose to about 35 psig and then dropped to zero. The temperature was held at 29-35C for 6 h. The foUowing day the reactor was discharged to afford 60.7 g of a clear supernatant over a brown soUd. Analysis of the product by GC and GC-MS indicated the following composition: Component GC Area % CC1F=CF2 5.8 CBrF2CClF2 1.7 cyclo-C4C12F6 (2) 11.7 C2Br2ClF3 0.8 C3Br2ClF5 27.7 C3Br2ClF5 7.7 C5BrC12F7 1.3 C5BrC12F7 1.5 C5BrC12F7 1.4 5 C5BrC12F7 1.1 C3Br2ClF3 0.9 C5Br2C12F8 2.0 C5Br2C12F8 13.2 C5Br2C12F8 3.6 0 C5Br2C12F8 17.6 EXAMPLE 20 Hydrogenation of CF3CF2CC12CF2CF3 over Pd/C Catalyst A 15 inch (38.1 cm) x 3/8 inch (0.95 cm) "Hastelloy" nickel aUoy tube 5 was filled with 4.68 gm (about 13 mL) .5% Pd/C ground to 4/10 mesh. The catalyst was activated by heating at 120C for 135 min under a hydrogen flow of 50 seem, 8.3x10-7 m3/s). The temperature of the reaction was raised to 175C while decreasing the flow of H2 to 22 seem (3.7x10-7 m3/s) and increasing the flow of CF3CF2CC12CF2CF3 to 7.3 seem (1.2x10-7 m3/s). The gaseous effluent was found 0 to be 93% CF3CF2CH2CHFCF3, an over hydgrogenation product. EXAMPLE 21 Hydrogenation of CF3CF2CC12CF2CF3 over Pd/C Catalyst The reactor described in Example 20 was filled with 2.00 gm (about 5 6.0 cc) of .5% Pd/C ground to 4/10 mesh. The catalyst was activated by heating at 150C for 52 min. under a hydrogen flow of 50 seem, 8.3x10-7 m3/s). The temperature of the reaction was lowered to 100C while decreasing the flow of H2 to 3.8 seem (6.3x10-8 m3/s) and increasing the flow of CF3CF2CC12CF2CF3 to 2.0 seem (3.3x10-8 m3/s). The gaseous effluent was found to be 57% o CF3CF2CH2CHFCF3, 9.4% CF3CF2CHC1CF2CF3, 16% CF3CF = CHCF2CF3, 4.8% CF3CF2CH2CF2CF3, 2.8% CF3CF=CC1CF2CF3, 1.5% CF3CHFCHC1CF2CF3, as weU as other unidentified by-products. EXAMPLE 22 Hydrogenation of CF3CF2CC12CF2CF3 over Pd/A12Q3 Catalyst The reactor described in Example 20 was filled with 3.48 gm (about 6.0 cc) of .5% Pd/A1203 (Calsicat 1/8" peUets #64A-057) ground to 4/10 mesh. The catalyst was activated by heating at 100C for 50 min. under a hydrogen flow of 50 seem, 8.3x10-7 m3/s). The temperature of the reaction was raised to 150C while decreasing the flow of H2 to 20 seem (3.3x10-7 m3/s) and increasing the flow of CF3CF2CC12CF2CF3 to 10.0 seem (1.7x10-7 m3/s). The gaseous effluent was found to be 61% CF3CF2CHC1CF2CF3, which can recycled, 25% CF3CF2CH2CF2CF3, 3.1% CF3CF=CC1CF2CF3, < 1% CF3CHFCH2CF2CF3, While certain aspects of the invention have been described in particular detail a person in this art would recognize that other aspects and embodiments are encompassed by the appended claims.

Claims: 5 THE FOLLOWING IS CLAIMED: 1. A process for making perhalopropanes and/or pentanes which comprises: (i) contacting (a) a dihalodifluoromethane, CXYF2, where X and Y are independently Cl or Br, with 0 (b) a fluoroolefin which is at least one of tetrafluoroethylene and chlorotrifluoroethylene, in the presence of (c) a modified aluminum chloride catalyst under addition condensation conditions to produce (d) at least one of a perhalofluoropropane having 5 to 6 fluorine and 2 to 5 3 nonfluorohalogen substituents totalling 8 halogens and (e) a perhalofluoropentane having 8 to 10 fluorine and 2 to 4 nonfluorohalogen substituents totalling 12 halogen substituents, the fluorine content of said propanes and pentanes being the sum of the fluorine contents of the (a) and (b) reactants; and 0 (ii) recovering at least one of said perhalopropanes and pentanes. 2. The process of Claim 1 wherein the modified catalyst is produced before said catalyst is contacted with said reactants. 5 3. The process of Claim 1 wherein the modified catalyst is produced in situ. 4. The process of Claim 1 wherein the fluoroolefin comprises TFE, the propane when produced has the formula C3XYF6, and the pentane when o produced has the formula C5XYF10. 5. The process of Claim 1 wherein the CXYF2 reactant comprises CC12F2 and at least one propane when produced has the formula C3C12F6, and at least one pentane when produced has the formula C5C12F10. 5 6. The process of Claim 5 wherein said C3C12F6 comprises one or more of CC12FCF2CF3 and CC1F2CCF2CC1F2; and said C5C12F10 comprises one or more of C2F5CC12C2F5 and CF3CC12CF2CF2CF3. 7. The process of Claim 1 wherein the CXYF2 comprises CBrClF2 and said perhalofluoropropane and perhalofluoropentane comprise one or more isomers having the forumula C3BrClF6 and C5BrClF10. 8. The process of Claim 8 wherein the propane isomers comprise at least one member from the group consisting of CBrF2CF2CClF2, CBrClFC2F5, CF3CBrFCClF2, and CF3CBrClCF3, and the pentane isomers comprise at least one member from the group consisting of C2F5CBrClC2F5, and CF3CBrClCF2CF2CF3. 9. The process of Claim 1 wherein the CXYF2 reactant comprises CBr2F2, and the reaction product mixture comprises at least one of a perbromofluoropropane and a perbromofluoropentane, wherein the perbromofluoropropane comprises one or more isomers having the forumula C3Br2F6 and the perbromofluoropentane comprises one or more isomers having the formula C5Br2F10. 10. The process of Claim 9 wherein the propane isomers comprise at least one of CBrF2CF2CBrF2 and CBr2FC2F5, and the pentane isomers comprise at least one of C2F5CBr2C2F5 and CF3CBr2CF2CF2CF3. 11. The process of Claim 1 wherein the CXYF2 reactant comprises CBr2F2, the catalyst comprises aluminum chloride, and the reaction mixture comprises at least one of perhalofluoropropane having the formula C3BrClF6 and a perhalofluoropentane having the formula C5BrClF10. 12. The process of Claim 11 wherein the C3BrClF6 comprises one or more of CBrF2CF2CClF2, CBrClFC2F5, and CF3CBrClCF3; and the C5BrClF10 comprises C2F5CBrClC2F5. 13. The process of Claim 1 wherein the fluoroolefin reactant comprises CTFE, and the propane product has the formula C3C1XYF5, and the pentane product having 8 fluorine and 4 nonfluorohalogen substituents has the formula C5C12XYF& 14. The process of Claim 13 wherein the CXYF2 reactant comprises CC12F2, the propane reaction product comprises C3CBF5, and the pentane reaction product comprises C5C14F8. 15. The process of Claim 14 wherein the C3CBF5 product comprises one or more of CC1-F2CC1FCC1F2, CC12FCC1FCF3, CC12FCF2CC1F2, and CCBCF2CF3; and the C5C14F8 reaction product comprises one or more of CF3CC1FCC12CC1FCF3, CαF2CClFCF2CC12CF3, and CC1F2CF2CC12CF2CC1F2. 16. The process of Claim 1 wherein the CXYF2 reactant comprises CBrClF2, the propane reaction product comprises C3BrC12F5 and the pentane reaction product comprises C5BrCBF8. 17. The process of Claim 16 wherein the C3BrC12F5 comprises one or more of CBrF2CClFCClF2, CBrClFCF2CClF2, and CF3CBrClCClF2. 18. The process of Claim 14 wherein the CXYF2 reactant comprises CBr2F2, the propane reaction product comprises C3Br2ClF5 and the pentane reaction product comprises C5Br2C12F8. 19. The process of Claim 18 wherein the C3Br2ClF5 propane reactioin product comprises one or more of CBr2FCClFCF3 and CBr2FCF2CClF2, and C5Br2C12F8. 20. A composition of matter comprising at least one of a perhalofluoropropane and a perhalofluoropentane, the propane having 5 to 6 fluorine, 2 to 3 nonfluorohalogen substituents at least one of which is bromine and a total of 8 halogens, the pentane having 8 to 10 fluorines, 2 to 4 nonfluorine halogen substitutents, at least one of which is bromine and a total of 10 halogens. 21. The composition of Claim 20 wherein the composition comprises at least one member from the group consisting of CClF2CF2CBrClF, CBrC12CF2CF3 and CBrF2CF2CC12F; CBr3CF2CF3 and CBrF2CBr2CF3; CC1F2CC1FCF2CC12CF3 and CC1F2CF2CC12CF2CC1F2; C5Br2C12F8 isomers; CC1F2CF2CC12CF2CF3, C5BrC12F9 isomers; C5Br2ClF9 isomers; _ _ CBrF2CF2CBr2CF2CF3; C2F5CC12C2F5 and CF3CC12CF2CF2CF3; C2F5CBrClC2F5 and CF3CBrClCF2CF2CF3;C2F5CBr2C2F5 and CF3CBr2CF2CF2CF3. 22. A process for hydrogenating the recovered perhalofluoropropanes or pentanes of Claim 1 which process comprises: (i) contacting at least one of said propane and pentane with molecular hydrogen in the presence of a Group V-QI metal hydrogenation catalyst at a temperature and pressure effective to result in the replacement of at least one nonfluorohalogen substituent with a hydrogen substituent, thereby forming a hydrogenated propane or pentane containing at least one more hydrogen substituent and at least one less nonfluorohalogen substituent, and (n) recovering said hydrogenated propane or pentane. 23. The process of Claim 22 wherein said contacting of step (i) is carried out in the vapor phase over a palladium catalyst. 24. The process of Claim 22 wherein the palladium is supported on carbon or alumina. 25. The process of Claim 24 wherein the support comprises alumina.

Inventors: NAPPA MARIO JOSEPH, SIEVERT ALLEN CAPRON, NAPPA, MARIO, JOSEPH, SIEVERT, ALLEN, CAPRON
Applicants: DU PONT, E.I. DU PONT DE NEMOURS AND COMPANY
Application year: 1994
Main classification: C07C17
IPC codes: B01J23, B01J27, C07B61, C07C17, C07C19